JPH0470242B2 - - Google Patents
Info
- Publication number
- JPH0470242B2 JPH0470242B2 JP59196975A JP19697584A JPH0470242B2 JP H0470242 B2 JPH0470242 B2 JP H0470242B2 JP 59196975 A JP59196975 A JP 59196975A JP 19697584 A JP19697584 A JP 19697584A JP H0470242 B2 JPH0470242 B2 JP H0470242B2
- Authority
- JP
- Japan
- Prior art keywords
- hydrochloric acid
- oxy
- superheated
- hcl
- reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 71
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 21
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 20
- 238000002485 combustion reaction Methods 0.000 claims abstract description 13
- 238000010791 quenching Methods 0.000 claims abstract description 9
- 150000008280 chlorinated hydrocarbons Chemical group 0.000 claims abstract description 8
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000004519 manufacturing process Methods 0.000 claims abstract description 6
- 238000004821 distillation Methods 0.000 claims description 8
- 230000000171 quenching effect Effects 0.000 claims description 8
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 6
- 239000005977 Ethylene Substances 0.000 claims description 6
- 238000005660 chlorination reaction Methods 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 5
- 239000000460 chlorine Substances 0.000 claims 1
- 229910052801 chlorine Inorganic materials 0.000 claims 1
- 238000011084 recovery Methods 0.000 abstract 1
- 239000002253 acid Substances 0.000 description 8
- 239000007789 gas Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000003795 desorption Methods 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、塩素化炭化水素の残渣から、特に塩
化ビニルの製造からの塩素化炭化水素の残渣か
ら、塩化水素を回収する方法並びに、特に該方法
を実施するための、装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention provides a method for recovering hydrogen chloride from residues of chlorinated hydrocarbons, in particular from residues of chlorinated hydrocarbons from the production of vinyl chloride, and in particular a method for carrying out the method. , regarding the device.
ドイツ特許出願公開第2314786号明細書から、
VC−プラントの廃ガスを燃焼させ、燃焼で生じ
たHClを急冷装置で冷却し、吸収させて塩酸にす
ることが既に知られている。 From German Patent Application No. 2314786,
It is already known to combust waste gas from a VC plant, cool the HCl produced by the combustion in a quenching device, and absorb it into hydrochloric acid.
既知の方法の欠点は特に、約30％に濃縮した後
でも塩酸が比較的無価値の生成物であるというこ
とである；なぜなら当該技術水準から明らかなよ
うに、酸にされた塩化水素は、装置的に非常に費
用のかかる脱着によつてだけ、VC−製造工程に
送還することができるからである。 A disadvantage of the known process is, inter alia, that hydrochloric acid is a relatively worthless product even after concentration to about 30%; since, as is clear from the state of the art, acidified hydrogen chloride This is because it can only be returned to the VC production process by desorption, which is very expensive in terms of equipment.
既知の方法の他の大きな欠点は、そこで記載さ
れた底部液での脱着で共沸混合物の酸を蒸留しな
ければならないので、脱着に使用されたHClの約
三分の一が失われるということである。更に、薄
い酸では、即ち共沸混合物以下では、一層多量の
水を、オキシ−反応器の後に接続した洗浄装置ま
たは蒸留装置で分離しなければならないというこ
とがある。又、腐食の危険が増す。 Another major drawback of the known method is that the azeotrope acid has to be distilled off in the desorption in the bottom liquid as described therein, so that approximately one-third of the HCl used in the desorption is lost. It is. Furthermore, with dilute acids, ie below the azeotrope, it may be the case that more water has to be separated off in a washing or distillation device connected after the oxy-reactor. Also, the risk of corrosion increases.
本発明の課題は、先ず記載した費用のかかる方
法を避け且つ、塩酸から塩化水素をたやすく回収
しうるようにする溶液を供給することである。 The object of the invention is to provide a solution which avoids the expensive process described in the first place and which makes it possible to easily recover hydrogen chloride from hydrochloric acid.
類による方法を用いてこの課題は本発明では、
残渣の燃焼及び後続の急冷用循環から出た塩酸を
先ず蒸発させ、次に過熱させ且つ次にオキシ塩素
化−反応器にじかに供給することによつて解決さ
れる。 In the present invention, this problem is solved using the method according to
The solution is to first evaporate the hydrochloric acid leaving the combustion of the residue and the subsequent quenching cycle, then superheat it and then feed it directly to the oxychlorination reactor.
本発明による方法では、幾つかの利点が生じ
る：
残渣の燃焼は、０〜100％の負荷のオキシ−塩
素化と無関係に行うことができる。カトキシド法
（Catoxydprozeβ）のような既知の方法では、オ
キシ−塩素化が行われないか装入量が通常値の50
％以下に減少した場合に、装置の運転を止めなけ
ればならない。本発明による方法の他の長所は、
望ましい場合にはいつでも塩酸の製造に切換える
ことができるということである。塩酸が非常に腐
食性の媒質であるということから生じる、専門の
世界で主張されるじかに塩酸を供給するちゆうち
よも本発明で取りのけることができる。 Several advantages arise in the process according to the invention: The combustion of the residue can be carried out independently of the oxy-chlorination with a load of 0 to 100%. In known methods such as the catoxide process (Catoxydprozeβ), oxy-chlorination does not take place or the charge is
%, the equipment must be shut down. Other advantages of the method according to the invention are:
This means that it is possible to switch to the production of hydrochloric acid whenever desired. The difficulties advocated in the professional world of directly supplying hydrochloric acid, resulting from the fact that hydrochloric acid is a highly corrosive medium, can also be avoided with the present invention.
実施態様において本発明は、蒸発及び過熱に高
濃度の塩酸を使用することを前もつて考慮する；
それによつて処理の効率を高めることができる。 In embodiments, the invention contemplates the use of highly concentrated hydrochloric acid for evaporation and superheating;
Thereby, processing efficiency can be increased.
本発明は、過熱した塩酸に塩化ビニルの蒸留か
らの送還したHClを混合することも前もつて考慮
する；その際他の実施態様において、過熱した塩
酸をVC−蒸留から出た返送HClとそしてエチレ
ンとの共通の導管でオキシ−反応器に供給するこ
とを前もつて考慮することができる。 The invention also contemplates mixing the superheated hydrochloric acid with the recirculated HCl from the distillation of vinyl chloride; in other embodiments, the superheated hydrochloric acid is mixed with the recirculated HCl from the VC-distillation; It can be envisaged beforehand to feed the oxy-reactor in a common line with ethylene.
特に最後の方法は、非耐酸性に設計された反応
器でも本方法を実施することができるということ
を前提とする；というのは、本発明による混合物
は腐食を少なくするか又は全くしめ出すからであ
る。 The last method in particular presupposes that the method can also be carried out in reactors designed to be non-acid resistant, since the mixture according to the invention exhibits less or no corrosion. It is.
本発明は、酸の容器とオキシ−塩素化の反応器
との間に少なくとも一つの熱交換器を塩酸の蒸発
及び過熱のためにあらかじめ備えることによつて
前記課題を解決する、特に前記方法の実施のため
の、装置も前もつて考慮する。 The invention solves this problem by pre-provisioning at least one heat exchanger between the acid container and the oxy-chlorination reactor for the evaporation and superheating of the hydrochloric acid. Consider the equipment for implementation in advance.
この装置で、今まで必要な費用のかかる装置の
部分を避ける。同時に、濃厚な酸を使用すること
ができるので、後続の精製において比較的少量の
水を分離しなければならない。更に、当該技術水
準の場合と同様に、オキシ−反応器と燃焼室との
間にじかにガスを供給する；それによつて比較的
安全な運転が保証される。 With this device, you avoid the costly pieces of equipment that were previously required. At the same time, concentrated acids can be used, so that relatively small amounts of water have to be separated off in the subsequent purification. Furthermore, as is the case in the state of the art, gas is supplied directly between the oxy-reactor and the combustion chamber; a relatively safe operation is thereby ensured.
本発明は又、過熱したHClと、VCの蒸留から
の反送HClと、エチレンとを供給するために共通
の供給管をオキシ−反応器にあらかじめ備えるこ
とを前もつて考慮する。この方策は更に又、全装
置を簡単化する。 The invention also provides for pre-equipping the oxy-reactor with a common feed line for feeding superheated HCl, recirculated HCl from the distillation of VC and ethylene. This measure also simplifies the overall device.
他の装置の部分との接続で、装置を簡単な送風
機で運転することができるようになる一方、カト
キシド−または圧縮−燃焼の際にコンプレツサー
が必要である。又、比較的小さい燃焼用空気の送
風機を使用することができるので、ことごとくは
るかに経済的な運転を行うことができ、それによ
つて特に、HClを循環に導くことが経済的にな
る。 In connection with other plant parts, it is possible to operate the plant with a simple blower, whereas in the case of catoxide or compression combustion a compressor is required. In addition, a relatively small combustion air blower can be used, which makes the operation much more economical overall, which makes it particularly economical to circulate the HCl.
本発明を次に図面によつて例として詳細に説明
する；その際図面は、簡単化して描写した装置の
接続図を示す。 The invention will now be explained in more detail by way of example with the aid of the drawings, which show connection diagrams of the device in a simplified manner.
導管１によつて液状残渣をそして導管２によつ
て廃ガス並びに追加的に空気及び水を燃焼室３に
供給し、そこで燃焼させる。 The liquid residue is supplied via line 1 and the waste gas and additionally air and water are fed via line 2 to the combustion chamber 3, where it is combusted.
生じた煙ガスは、導管４によつて急冷装置５に
供給される。同時に急冷装置５に導管６によつて
塩酸を、煙ガスの冷却のために供給する。含まれ
ているHClは、導管８によつて吸収装置９に供給
され、吸収装置９で吸収されて濃塩酸になり、こ
の濃塩酸は酸のタンク１０等に集められる。 The resulting smoke gas is fed via conduit 4 to a quenching device 5 . At the same time, the quenching device 5 is supplied with hydrochloric acid via line 6 for cooling the smoke gases. The contained HCl is supplied via conduit 8 to an absorption device 9 where it is absorbed into concentrated hydrochloric acid, which is collected in an acid tank 10 or the like.
酸はそこから導管６を経て、記載したように、
急冷装置５にもどる。導管１１を経て塩酸の他の
部分が、記載した例では先ず熱交換器１２で蒸発
せしめられ且つ他の熱蒸発装置１３で過熱せしめ
られる。 The acid then passes through conduit 6 and, as described,
Return to quenching device 5. A further portion of the hydrochloric acid via line 11 is, in the example described, first evaporated in a heat exchanger 12 and superheated in a further thermal evaporation device 13 .
単一の熱交換器でも蒸発及び過熱させることが
できるということは自明である。このことは点と
棒との線で表わし、参照記号１４を与えた。 It is self-evident that evaporation and superheating can be achieved even with a single heat exchanger. This is represented by a dot-bar line and given the reference symbol 14.
過熱した酸の蒸気は導管１４を経て導管１６に
供給される；該導管１６はオキシ−反応器１７に
行き当たる。同時に導管１６に、導管１８を経て
VC−蒸留からの返送HClが供給され、全く同様
に導管１９を経てエチレンが供給される。 The superheated acid vapor is fed via line 14 into line 16; said line 16 impinges on oxy-reactor 17. At the same time, through conduit 16 and conduit 18
Recycle HCl from the VC-distillation is fed in, and ethylene is fed in exactly the same way via line 19.
オキシ−反応器１７でHClはO2及びC2H4と一
緒に触媒の存在下で反応してジクロルエタンにな
り、そこで導管２０を経て取り除かれ、他の工程
に供給される。 In the oxy-reactor 17 the HCl reacts with O 2 and C 2 H 4 in the presence of a catalyst to form dichloroethane, which is removed via line 20 and fed to other steps.
もちろん、記載した本発明の実施例は、更に
種々の点で、根本思想から離れずに変更すること
ができる。それ故本発明は特に、既に記載したよ
うに、熱交換器を縦に二つ並べる組立の仕方だけ
に制限されない。組立の仕方に応じてこの場合、
熱交換器の塔、並列及び直列に接続した熱交換器
等をあらかじめ備えることができる。ずつと上に
記載したように、使用されるべき送風機及びポン
プを比較的小さくすることができる。概観の理由
でこれらの集合体は原理のスケツチにおいて別々
に記載しなかつた。 Of course, the embodiments of the invention described may be further modified in various respects without departing from the underlying idea. The invention is therefore not limited, in particular, to the way of assembling two heat exchangers one after the other, as already mentioned. In this case, depending on how it is assembled,
A column of heat exchangers, heat exchangers connected in parallel and series, etc. can be provided in advance. As mentioned above, the blowers and pumps to be used can be relatively small. For reasons of overview, these assemblies have not been described separately in the principle sketch.
図は、本発明による装置の一実施例を示す図で
ある。
１……塩素化炭化水素の残渣を燃焼室３に供給
する導管、２……廃ガス、空気及び水を燃焼室３
に供給する導管、３……燃焼室、４……煙ガスの
導管、５……急冷装置、８……HClの導管、９…
…吸収装置、１０……塩酸のタンク、１１……塩
酸の導管、１４……塩酸を蒸発及び過熱させる熱
交換器、１６……共通の導管、１７……オキシ−
塩素化−反応器。
The figure shows an embodiment of the device according to the invention. 1... Conduit for supplying chlorinated hydrocarbon residues to the combustion chamber 3, 2... Conduit for supplying waste gas, air and water to the combustion chamber 3
3... Combustion chamber, 4... Smoke gas conduit, 5... Quenching device, 8... HCl conduit, 9...
...Absorption device, 10...tank for hydrochloric acid, 11...conduit for hydrochloric acid, 14...heat exchanger for evaporating and superheating the hydrochloric acid, 16...common conduit, 17...oxy-
Chlorination - Reactor.
Claims (1)
造からの塩素化炭化水素の残渣から塩化水素を回
収する方法にして、残渣の燃焼及び後続の急冷用
循環から出た塩酸を先ず蒸発させ、次に過熱させ
且つ次にオキシ−塩素化−反応器にじかに供給す
ることを特徴とする方法。 ２ 蒸発及び過熱に高濃度の塩酸を使用する、特
許請求の範囲第１項記載の方法。 ３ 過熱した塩酸に、塩化ビニルの蒸留からの送
還したHClを混合する、特許請求の範囲第１項又
は第２項記載の方法。 ４ 過熱した塩酸を、VC−蒸留から出た返送
HClとエチレンとの共通の導管でオキシ反応器に
供給する、特許請求の範囲第１項又は第２項記載
の方法。 ５ 塩酸のタンク１０とオキシ−塩素化−反応器
１７との間に少なくとも一つの熱交換器１４を、
塩酸の蒸発及び過熱のためにあらかじめ備えたこ
とを特徴とする−特に、塩素化炭化水素の残渣、
特に塩化ビニルの製造からの塩素化炭化水素の残
渣、から塩化水素を回収するために残渣の燃焼及
び後続の急冷用循環から出た塩酸を先ず蒸発さ
せ、次に過熱させ且つ次にオキシ−塩素化−反応
器にじかに供給する方法を実施するための−装
置。 ６ 過熱したHClと、VCの蒸留からの返送HCl
と、エチレンとを一緒に供給するために、共通の
供給管１６をオキシ−反応器１７にあらかじめ備
えた、特許請求の範囲第５項記載の装置。[Scope of Claims] 1. A method for recovering hydrogen chloride from residues of chlorinated hydrocarbons, in particular from residues of chlorinated hydrocarbons from the production of vinyl chloride, comprising hydrochloric acid from combustion of the residue and subsequent quenching circulation. A process characterized in that it is first evaporated, then superheated and then fed directly to the oxy-chlorination reactor. 2. The method according to claim 1, in which highly concentrated hydrochloric acid is used for evaporation and superheating. 3. The method according to claim 1 or 2, wherein the superheated hydrochloric acid is mixed with HCl recycled from the distillation of vinyl chloride. 4 Return superheated hydrochloric acid from VC-distillation
3. A process as claimed in claim 1 or claim 2, in which HCl and ethylene are fed in a common conduit to the oxy reactor. 5 at least one heat exchanger 14 between the hydrochloric acid tank 10 and the oxy-chlorination reactor 17;
characterized by pre-provision for evaporation and superheating of hydrochloric acid - in particular residues of chlorinated hydrocarbons,
In order to recover hydrogen chloride from residues of chlorinated hydrocarbons, particularly from the production of vinyl chloride, the hydrochloric acid leaving the combustion of the residue and the subsequent quenching cycle is first evaporated, then superheated and then the oxy-chlorine - Apparatus for carrying out the process of directly feeding the reactor. 6 Superheated HCl and return HCl from VC distillation
6. The device as claimed in claim 5, wherein the oxy-reactor 17 is provided with a common supply pipe 16 for jointly feeding ethylene and ethylene.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3334677.1 | 1983-09-24 | ||
| DE19833334677 DE3334677A1 (en) | 1983-09-24 | 1983-09-24 | METHOD AND PLANT FOR RECOVERING CHLORINE FROM CHLORINE HYDROCARBON RESIDUES |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60221302A JPS60221302A (en) | 1985-11-06 |
| JPH0470242B2 true JPH0470242B2 (en) | 1992-11-10 |
Family
ID=6210013
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59196975A Granted JPS60221302A (en) | 1983-09-24 | 1984-09-21 | Method and device for recovering hydrogen chloride from chlorinated hydrocarbon residue |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0137160B1 (en) |
| JP (1) | JPS60221302A (en) |
| AT (1) | ATE29476T1 (en) |
| DE (2) | DE3334677A1 (en) |
| SU (1) | SU1572411A3 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2139237C1 (en) * | 1998-05-29 | 1999-10-10 | Акционерное общество открытого типа "ВСЕРОССИЙСКИЙ АЛЮМИНИЕВО-МАГНИЕВЫЙ ИНСТИТУТ" АО ВАМИ | Method of production of hydrogen chloride and furnace for its embodiment |
| RU2173296C2 (en) * | 1999-07-29 | 2001-09-10 | Акционерное общество открытого типа "Всероссийский алюминиево-магниевый институт" | Hydrogen chloride production process and furnace for implementation of the process |
| RU2159734C1 (en) * | 2000-04-13 | 2000-11-27 | Марат Аронович Гликин | Method of processing liquid chlorine-containing waste from vinyl chloride production |
| RU2430013C1 (en) * | 2010-03-04 | 2011-09-27 | ОАО "Сибур-Нефтехим" | Method of producing hydrochloric acid |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL6706807A (en) * | 1967-05-17 | 1967-07-25 | ||
| FR1595619A (en) * | 1967-09-25 | 1970-06-15 | ||
| US3816599A (en) * | 1971-11-16 | 1974-06-11 | Lummus Co | Hydrogen chloride recovery |
| US3968200A (en) * | 1972-03-27 | 1976-07-06 | The Lummus Company | Reactor effluent quench system |
| US3980758A (en) * | 1972-12-22 | 1976-09-14 | Hoechst Aktiengesellschaft | Process for the combustion of chlorine containing wastes |
| US3950443A (en) * | 1973-09-27 | 1976-04-13 | Prahl Walter H | Utilization of waste products containing chlorine in the production of chlorinated organic compounds by combination of oxychlorination with combustion |
| US4157380A (en) * | 1976-11-26 | 1979-06-05 | Prahl Walter H | Recovery of hydrogen chloride and chlorine from chlorine-containing organic wastes |
| US4351819A (en) * | 1981-01-26 | 1982-09-28 | The Lummus Company | Recovery of chlorine values in integrated process for oxychlorination and combustion of chlorinated hydrocarbons |
| US4346069A (en) * | 1981-01-26 | 1982-08-24 | The Lummus Company | Recovery of chlorine values in integrated process for oxychlorination and combustion of chlorinated hydrocarbons |
-
1983
- 1983-09-24 DE DE19833334677 patent/DE3334677A1/en not_active Withdrawn
-
1984
- 1984-07-25 AT AT84108798T patent/ATE29476T1/en active
- 1984-07-25 DE DE8484108798T patent/DE3465971D1/en not_active Expired
- 1984-07-25 EP EP84108798A patent/EP0137160B1/en not_active Expired
- 1984-09-10 SU SU843788058A patent/SU1572411A3/en active
- 1984-09-21 JP JP59196975A patent/JPS60221302A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| SU1572411A3 (en) | 1990-06-15 |
| DE3465971D1 (en) | 1987-10-15 |
| EP0137160B1 (en) | 1987-09-09 |
| JPS60221302A (en) | 1985-11-06 |
| EP0137160A1 (en) | 1985-04-17 |
| DE3334677A1 (en) | 1985-04-18 |
| ATE29476T1 (en) | 1987-09-15 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EXPY | Cancellation because of completion of term |